Combined steam reformation reactions and water gas shift reactions for on-board hydrogen production in an internal combustion engine

Abstract

The present disclosure relates to an apparatus and method for increasing the level of hydrogen produced in an exhaust gas recirculation pathway within an internal combustion engine. A hydrocarbon water gas shift reformer is positioned in series with a water gas shift reformer within the exhaust gas recirculation pathway to improve the yield of hydrogen and to improve the relative efficiency of both catalytic procedures.

Claims

1. A method to process exhaust gas expelled from at least one cylinder of a plurality of cylinders of an internal combustion engine, the method comprising: (a) providing an internal combustion engine having an intake manifold wherein the engine includes an exhaust gas recirculation pathway containing a hydrocarbon steam reformer including a steam reformation catalyst and a water gas shift reformer including a water gas shift catalyst wherein said water gas shift reformer is serially coupled downstream of said hydrocarbon steam reformer; (b) introducing hydrocarbon fuel and air into one or more cylinders of the engine; (c) operating the engine such that internal combustion occurs in one or more cylinders of the engine and generating an untreated exhaust gas in one or more cylinders of the engine and expelling said untreated exhaust gas from said one or more cylinders wherein the untreated exhaust gas contains: (1) unreacted hydrocarbon fuel and water; or (2) water and no hydrocarbon fuel; (d) determining a level of hydrocarbon in said untreated exhaust gas with a hydrocarbon sensor; (e) based on said level of hydrocarbon determined by said hydrocarbon sensor, i) in the case that the untreated exhaust gas contains unreacted hydrocarbon and water, optionally introducing additional hydrocarbon to the untreated exhaust gas and ii) when said untreated exhaust gas contains water and no hydrocarbon, introducing hydrocarbon to the untreated exhaust gas to provide a treated exhaust gas, wherein both the untreated and treated exhaust gas contain hydrocarbon and water, wherein said level of hydrocarbon is set in the range of 1.0% to 5.0% by volume; (f) introducing the untreated and/or treated exhaust gas into the hydrocarbon steam reformer and reacting the hydrocarbon and water in the untreated and/or treated exhaust gas in the presence of the steam reformation catalyst at a temperature of 400° C. to 800° C. and outputting an exhaust gas containing increased levels of carbon monoxide and hydrogen, and wherein said hydrogen in said exhaust gas output after said reaction in said water gas shift reformer is at a level of 2.0% by volume to 10.0% by volume; (g) introducing the exhaust gas output from step (e) to said water gas shift reformer and reacting the carbon monoxide and water in said exhaust gas output in the presence of the water gas shift catalyst and forming carbon dioxide and hydrogen; and (h) introducing said exhaust gas output to said intake manifold of said engine.

2. The method of claim 1 wherein the hydrogen gas in said untreated exhaust gas is at a level of 0.1% by volume to 6% by volume.

3. The method of claim 1 wherein said steam reformation catalyst in said hydrocarbon steam reformer is maintained at said temperature of 400° C. to 800° C. exclusively by generation of heat from said internal combustion engine.

4. The method of claim 1 wherein said engine includes a cylinder block and said hydrocarbon steam reformer is positioned at a distance of 3.0 inches to 24.0 inches from said cylinder block.

5. The method of claim 1 wherein operating the engine such that internal combustion occurs in one or more cylinders of the engine further comprises operating the engine such that at least one of the cylinders of the engine is a dedicated exhaust gas recirculation (D-EGR) cylinder.

6. The method of claim 1 wherein expelling the untreated exhaust gas from the cylinders of the engine includes expelling the untreated exhaust gas from the dedicated exhaust gas recirculation cylinder and the untreated exhaust gas expelled from the dedicated exhaust gas recirculation cylinder is introduced to said hydrocarbon steam reformer followed by said water gas shift reformer.

7. The method of claim 1 wherein at least one cylinder of said internal combustion engine is a dedicated exhaust gas recirculation (D-EGR) cylinder, wherein 90% to 100% by volume of the exhaust gas expelled from the dedicated EGR cylinder is recirculated in said exhaust gas recirculation pathway containing said hydrocarbon steam reformer and said water gas shift reformer connected in series.

8. The method of claim 1 wherein said internal combustion engine includes a turbine and said exhaust gas recirculation pathway comprises a high-pressure exhaust gas recirculation system wherein a portion of said exhaust gas is taken upstream of the turbine and said exhaust gas is recirculated.

9. The method of claim 1 wherein said internal combustion engine includes a turbine and said exhaust gas recirculation pathway comprises a low-pressure exhaust recirculation system wherein a portion of said exhaust gas is taken downstream of the turbine and said exhaust gas is recirculated.

10. The method of claim 1 wherein said hydrocarbon fuel comprises methane and said water gas shift reaction comprises:
CH.sub.4+H.sub.2O.fwdarw.CO+3H.sub.2.

11. The method of claim 10 wherein said steam reformation catalyst is at a temperature of 500° C. to 800° C.

12. The method of claim 11 wherein said temperature of 500° C. to 800° C. is maintained exclusively by generation of heat from said internal combustion engine.

13. The method of claim 1 wherein said water gas shift reaction is conducted at a temperature of 300° C. to 500° C.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) The above-mentioned and other features of this disclosure, and the manner of attaining them, will become more apparent and better understood by reference to the following description of embodiments described herein taken in conjunction with the accompanying drawings, wherein:

(2) FIG. 1 illustrates the influence of hydrogen addition to the laminar burning velocity of a methane fueled flame.

(3) FIG. 2 illustrates the impact of carbon monoxide addition to the laminar burning velocity of a methane fueled flame.

(4) FIG. 3 illustrates a fuel reformer containing a water gas shift catalyst serially coupled downstream of a hydrocarbon steam reformer containing steam reformation catalyst as part of a four cylinder high pressure loop spark-initiated exhaust gas recirculation (EGR) system containing a dedicated exhaust gas recirculation cylinder.

(5) FIG. 4 illustrates the fractional conversion of methane at indicated temperatures due to the steam reformation reaction.

(6) FIG. 5 illustrates a fuel reformer containing a water gas shift catalyst serially coupled downstream of a hydrocarbon steam reformer containing steam reformation catalyst as part of high pressure loop EGR system.

(7) FIG. 6 illustrates a fuel reformer containing a water gas shift catalyst serially coupled downstream of a hydrocarbon steam reformer containing steam reformation catalyst as part of a low pressure loop EGR system.

DETAILED DESCRIPTION

(8) The present disclosure relates to both a method and apparatus for increasing the production of hydrogen (H.sub.2) in an exhaust gas recirculation system of any selected internal combustion engine. More specifically, the present disclosure relates to implementation of a serially coupled exothermic water gas shift reaction and endothermic steam reformation reaction, in an exhaust gas recirculation system, of an internal combustion engine, to increase the overall yield of H.sub.2 and ensuing engine efficiency. The internal combustion engines suitable for use herein are contemplated to include any hydrocarbon fueled engine, including but not limited to the use of gasoline, diesel and natural gas.

(9) In such context, reference is initially directed to FIG. 1, which illustrates and confirms that the addition of H.sub.2 to a representative CH.sub.4 fueled flame results in an increase in the burning velocity of the mixed flame. Attention is next directed to FIG. 2 which identifies the corresponding impact of CO on the laminar burning velocity of CH.sub.4. As can be seen, as CO concentrations are increased up to 15%, there is a corresponding observed increase in burning velocity. However, burning velocity is then observed to decrease as additional CO is added to the mixture. Accordingly, for the applicable range of H.sub.2 and CO concentration, the addition of both H.sub.2 and CO to the exhaust gas charge feed will increase the burning velocity of a given mixture, with the addition of H.sub.2 having, relatively speaking, a more significant effect. Accordingly, in order to further improve the yield of H.sub.2 in an internal combustion engine exhaust gas recirculation stream, it is disclosed herein that one may now serially couple a water gas shift catalyst downstream of a steam reformation catalyst. This then will now present a more efficient use of both chemical reaction profiles in an exhaust gas recirculation environment. The steam reforming reaction, which is a method for producing hydrogen and carbon monoxide from a hydrocarbon fuel in the presence of water, and as specifically applied to a natural gas fueled operation, is represented below:
CH.sub.4+H.sub.2O.fwdarw.CO+3H.sub.2

(10) The steam reforming reaction, as an endothermic reaction, may therefore be initially utilized to convert thermal energy to chemical energy in the form of H.sub.2 and CO. In the case of methane fuel, the reaction preferably takes place at temperatures at or above 500° C., or in the range of 500° C. to 800° C. As a result of this endothermic reaction, the temperature of the exhaust gas stream will be reduced to a value that is less than 500° C., such as in the range of 300° C. to 500° C.

(11) It is also worth noting that the steam reformation reaction utilized herein may also be applied in general to various hydrocarbon fuels, represented by the formula CnHm. In addition, the temperature range is more generally preferred to be in the range of 400° C. to 800° C., particularly for gasoline or diesel fuel systems. Accordingly, the more general description of the water gas shift reaction suitable for use herein is represented as follows:
CnHm+nH.sub.2O.fwdarw.nCO+(n+m/2)H.sub.2
In the above, the value of n and m are numerical values for a given hydrocarbon undergoing a steam reformation reaction. For example, in the case of methane, n=1 and m=4.

(12) The water gas shift (WGS) reaction is now summarized below:
CO+H.sub.2O.fwdarw.CO.sub.2+H.sub.2

(13) The water gas shift reaction above, in contrast to the steam reformation reaction, is mildly exothermic, meaning energy is released as the reaction progresses. This means that energy is lost through the process and the energy content of the H.sub.2 fuel is slightly less than energy content of the CO fuel. Additionally, the water gas shift catalyst exchanges CO for H.sub.2 meaning that any H.sub.2 produced results in the consumption of CO. It is therefore desirable to create both CO and H.sub.2 to achieve a maximum benefit of improved knock and EGR tolerance in a hydrocarbon fueled internal combustion engine.

(14) It is useful to note that one of the limitations of the water gas shift catalysts to produce H.sub.2 is that the thermodynamic equilibrium concentration of H.sub.2 and CO is a function of temperature. More specifically, increasing temperature increases the kinetic rate of the forward reaction, however at the same time it also shifts the thermodynamic equilibrium to the reactants. Preferably, therefore, the water gas shift catalyst is utilized herein at a temperature of 300° C. to 500° C. to augment the production of H.sub.2.

(15) Reference is made to FIG. 3 which identifies one example of the present disclosure where a water gas shift reformer containing a water gas shift catalyst is serially coupled downstream of a hydrocarbon steam reformer containing steam reformation catalyst as part of a four cylinder high pressure loop spark-initiated exhaust gas recirculation (EGR) system shown generally as item 10. Reference to a loop should be understood as providing in general a recirculation pathway for exhaust gases. One of the four cylinders is identified as the dedicated EGR (D-EGR) cylinder and is illustrated as such along with a port fuel injector (PFI) which therefore may optionally add to and/or enrich the relatively hot untreated exhaust output from the D-EGR cylinder with additional hydrocarbons to provide a treated exhaust gas mixture identified generally as Φ>1. A universal exhaust gas oxygen sensor is identified as UEGO. A heated exhaust gas oxygen sensor is identified as HEGO. A three-way catalytic converter is identified as TWC which may reduce nitrogen oxides to nitrogen and oxygen, oxidize carbon monoxide to carbon dioxide or provide oxidation of any unburnt hydrocarbons to carbon dioxide and water. In addition, it is noted that preferably 90% to 100% by volume of the exhaust gas expelled from the identified D-EGR cylinder is recirculated to the intake manifold.

(16) It should therefore be appreciated that after leaving the D-EGR cylinder the untreated exhaust gas and/or a treated exhaust gas (i.e. exhaust gas containing hydrocarbon supplied by the PFI) may then be introduced to the steam reformation catalyst reformer identified at 12. It is worth noting that the level of hydrogen gas in the exhaust gas just prior to introduction to the hydrocarbon steam reformer will can generally fall in the range of 0.1% to 6% by volume of the exhaust gas present.

(17) Accordingly, in the hydrocarbon steam reformer 12 any unburnt hydrocarbon and water vapor may undergo the steam reformation reaction. It is also useful to note that the port fuel injector may also include or be responsive to a separate hydrocarbon sensor such as a methane sensor to determine hydrocarbon levels in the untreated exhaust gas and automatically adjust such levels in the exhaust gas prior to introduction to the hydrocarbon steam reformer 12. Preferably, the level of hydrocarbons in the exhaust gas can then be set to fall in the range of 1.0% to 5.0% % by volume of the exhaust gas stream for treatment by the steam reformation catalyst.

(18) The exhaust gas emerging from the exhaust manifold, either itself containing unburnt hydrocarbons or no hydrocarbons, and optionally supplied with or enriched with hydrocarbons from the PFI, is therefore now readily introduced to the hydrocarbon steam reformer 12. Preferably, the hydrocarbon steam reformer 12 containing the steam reformation catalyst is selectively positioned such that the untreated and/or treated exhaust gases are introduced and exposed to elevated temperature such as at the preferred temperature range of at least 400° C. for gasoline or diesel operation, and preferably at a temperature of at least 500° C. for a natural gas type engine. Accordingly, the hydrocarbon steam reformer 12 is selectively positioned, taking into account any cooling of the untreated and/or treated exhaust gas stream that may occur prior to introduction to the steam reformation catalyst and in consideration of maintaining a relatively close proximity to the engine, so that the heat of the engine may now be exploited to maintain the exhaust gases at a temperature sufficient for the steam reformation reaction to proceed.

(19) The steam reformation catalyst herein preferably is selected from nickel (Ni) as the active metal. For example, the steam reformation catalyst may comprise Ni-M composition, where M=gold (Au), silver (Ag), tin (Sn), copper (Cu), cobalt (Co), molybdenum (Mo), iron (Fe), gadolinium (Gd) or boron (B). Apart from such N-M compositions, one may also use palladium (Pd) or platinum (Pt) as the steam reformation catalyst. A particularly preferred catalyst is nickel or palladium.

(20) The hydrocarbon steam reformer 12 containing steam reformation catalyst is preferably maintained at a distance in the range of 3.0 inches to 24.0 inches from the engine cylinder block 14. Accordingly, it is contemplated that the steam reformation catalyst herein can be exclusively heated to the temperatures of at least 400° C. to 800° C. by only engine heat due to engine internal combustion operation. In such manner, as noted, the temperatures of the untreated and/or treated exhaust gases are such that they are at the preferred temperatures for the steam reformation reaction to proceed at relatively efficient levels of conversion (e.g. greater than or equal to 50% conversion). In that regard, reference is made to FIG. 4 which, for the exemplary case of a methane fuel, identifies the fractional conversion of CH.sub.4 at the indicated temperature due to the steam reformation reaction. At 20 is shown the results of fractional CH.sub.4 conversion versus temperature in a membrane type reactor. A membrane type reactor is reference to a reactor that continuously removed hydrogen from the reacting stream. At 22 is illustrated the fractional conversion of CH.sub.4 for a packed bed reactor where there is no continuous removal of hydrogen. At 24 is the equilibrium situation which identifies the conversion of hydrocarbon to hydrogen at thermodynamic equilibrium. In the present disclosure, the hydrocarbon steam reformer may therefore assume either a membrane type configuration or packed bed configuration.

(21) Once the steam reformation reaction has taken place at 12, the exhaust gases, now containing CO and H.sub.2 due to the steam reformation reaction, are introduced to the water gas shift (WGS) reaction reformer at 16 (see again FIG. 3). Examples of WGS catalysts in the water gas shift reformer 16 preferably include iron oxides Fe.sub.3O.sub.4 or other transition metals and transition metal oxides. As noted herein, CO and H.sub.2O are then converted to CO.sub.2 and H.sub.2. Accordingly, ultimately introduced at the distribution mixer is an enriched level of hydrogen gas, which includes the additional hydrogen, created by the hydrocarbon steam reformer 12 and the water gas shift reformer 16. The amount of hydrogen gas introduced into the distribution mixer, for ensuing mixing with air and back into the intake manifold, will now contain a level of hydrogen gas of 2.0-10.0% by volume. As noted above, this amounts to a significant increase of the hydrogen in the exhaust gas emerging from the exhaust gas manifold, which as noted above, typically falls in the range of 0.1% to 6% by volume

(22) FIG. 5 illustrates another embodiment of the present disclosure as applied to a high-pressure loop EGR system (HPL-EGR). In such a system a portion of the exhaust gas is taken from upstream of the turbine as shown and ultimately reintroduced into the engine intake manifold. As can again be seen, the hydrocarbon steam reformer 26 is positioned such that it is relatively proximate to the engine such that the temperature can again be maintained in the range of 400° C. to 800° C. solely by the use of engine heat. A PFI is shown again for the optional introduction or enrichment of hydrocarbon to the exhaust gas. Following the steam reformation reaction once again the exhaust is serially coupled and introduced to the water gas shift reformer containing water gas shift catalyst shown generally at 28 followed by cooing by the EGR cooler and ultimately increased levels of H.sub.2 are now introduced to the Venturi mixed and eventually into the intake manifold.

(23) FIG. 6 illustrates yet another embodiment of the present disclosure as applied to a low-pressure loop EGR system (LPL-EGR). Reference to low pressure loop is reference to the feature that directs exhaust gas from the exhaust from a point on the exhaust line downstream of the turbine as shown to a point on the air intake line upstream from the compressor. Similar to the above, a PFI injector may be positioned to introduce hydrocarbons to the untreated exhaust gas prior to the hydrocarbon steam reformer shown generally at 30. Following the steam reformation catalyst reformer the exhaust gas is again serially routed through a water gas shift catalyst reformer shown generally at 32.

(24) It should be noted that with respect to any of the embodiments herein, operation in an environment that may contain significant levels of sulfur may be such that it can compromise the efficiency of the steam reformation catalyst. Accordingly, in such an environment, it is preferably to utilize a replaceable sulfur trap, or a sulfur trap capable of regeneration, upstream of the steam reformation catalyst in order to reduce or prevent excessive sulfur exposure of the steam reformation catalyst.

(25) As can now be appreciated from the above, by serially coupling a hydrocarbon steam reformer with a water gas shift reformer downstream of the steam reformer, there is relatively more efficient use of both catalytic procedures, as the production of H.sub.2 and CO is nearly zero at gas temperatures below 500° C. for methane as the hydrocarbon fuel. The steam reformation catalyst can be used to convert thermal energy to chemical energy in the form of H.sub.2 and CO. As a result of such endothermic reaction, the temperature of the exhaust gas stream is reduced to a value of less than 500° C. As the exhaust gas stream cools below 500° C., the thermodynamics are then favorable to the water gas shift production of H.sub.2 from CO and water.

(26) The foregoing description of several methods and embodiments has been presented for purposes of illustration. It is not intended to be exhaustive or to limit the claims to the precise steps and/or forms disclosed. It is intended that the scope of the invention be defined by the claims appended hereto.